CN104258709A - Waste derived fuel burning smoke separation and purifying process - Google Patents
Waste derived fuel burning smoke separation and purifying process Download PDFInfo
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- CN104258709A CN104258709A CN201410501011.8A CN201410501011A CN104258709A CN 104258709 A CN104258709 A CN 104258709A CN 201410501011 A CN201410501011 A CN 201410501011A CN 104258709 A CN104258709 A CN 104258709A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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Abstract
The invention relates to a waste derived fuel burning smoke separation and purifying process. The waste derived fuel burning smoke separation and purifying process comprises the following steps: filling an incinerator with oxygen, desulphurizing and denitrifying the smoke generated by the burning of the incinerator by utilizing ammonia water, rapidly cooling the desulphurized and denitrified smoke in a dry ice quench tower to prevent the generation of Dioxin, adsorbing heavy metals in the smoke by utilizing chelating agent in a cyclone dust collector, introducing slaked lime slurry into a semi-dry deacidification tower to deacidify the smoke, adsorbing impurity particles in the smoke by utilizing active carbon in an active carbon ejector, filtering dust particles through a film filter material in a bag-type dust collector, absorbing carbon dioxide in a hollow fiber micropore membrane filter tank by utilizing absorption liquid, heating smoke to 250 to 350 DEG C in a heating furnace, and discharging the smoke into atmosphere via a draught fan through a high chimney after various indexes are qualified. By adopting the waste derived fuel burning smoke separation and purifying process, harmful matters in the waste derived fuel burning smoke can be effectively separated and purified.
Description
Technical field
The present invention relates to flue gas isolation of purified technique, specifically refer to a kind of waste-derived fuel incineration flue gas isolation of purified technique.
Background technology
Waste-derived fuel burn have that calorific value is high, recovery utilization rate advantages of higher and being used widely.But the flue gas produced in burning process still containing many harmful substances, may cause the secondary pollution of environment.Harmful substances from flue gases main component comprises flue dust flying dust, sour gas (carbon monoxide, carbon dioxide, sulfur dioxide, sulfur trioxide, nitrogen oxide, hydrogen fluoride, hydrogen chloride etc.), particle, heavy metal, dioxin etc.How the flue gas that waste-derived fuel burns is carried out effective isolation of purified, to ensure that pollutant load is down to below standard limited value safety dumping again, when becoming design flue gas of refuse burning treatment system, need the difficult problem solved.
Summary of the invention
The object of the present invention is to provide a kind of waste-derived fuel incineration flue gas isolation of purified technique, by effective for the harmful substance in waste-derived fuel incineration flue gas isolation of purified.
The present invention is achieved through the following technical solutions: a kind of waste-derived fuel incineration flue gas isolation of purified technique, and its technological process comprises the step that next coming in order carry out:
A desulphurization denitration; Waste-derived fuel enters incinerator and burns, in incinerator, control temperature maintains more than 850 DEG C, the temperature of incinerator chamber exit end remains on 850 DEG C-1050 DEG C, flue gas is at the incinerator chamber exit end time of staying more than 2S, simultaneously, the top of incinerator chamber exit end uninterruptedly sprays ammoniacal liquor by ammonia spray device and is furnished with hoop combustion oxygen, and the ammonia fertilizer of generation falls into the conveyer belt of bottom;
The anti-dioxin of B; Heat smoke enters from the top of dry ice quench tower, and the tower wall along embedded dry ice flows from top to bottom, flue gas and the atomization quench water co-current contact sprayed into, and due to the rapid gasification of cold water and dry ice, heat smoke is cooled to less than 200 DEG C in 0.5S;
C removing heavy metals; Flue gas through chilling enters cyclone dust collectors from the bottom of dry ice quench tower, flue-gas temperature maintains 150 DEG C-200 DEG C, cyclone dust collectors top spray chelating agent solution, the heavy metal in chelating agent pressurized liquid spray and flue gas is thoroughly mixed to form particle, and particle falls to particle conveyor;
The depickling of D half dry type; Flue gas enters from half dry type extracting tower bottom, bottom half dry type extracting tower, rotary sprayer sprays slaked lime slurry downwards, the flue gas adverse current of slaked lime slurry solution and rising, react with the acidic materials in flue gas and generate dry powder shape material, powder falls to particle conveyor, and flue-gas temperature is down to less than 130 DEG C;
E particle-removing thing; Flue gas enters the activated carbon eductor between half dry type extracting tower and sack cleaner, sprays powdered activated carbon by activated carbon eductor in flue, and the activated carbon granule of adsorbing contaminant falls to particle conveyor from activated carbon eductor lower end;
F adsorbs flue dust; Flue gas enters from sack cleaner bottom, and temperature controls more than 60 DEG C, and in sack cleaner, Film Filter Materials filters;
G removing carbon dioxide; Faintly acid gas enters hollow fiber microporous membrane filtering tank, temperature controls at 40 DEG C-50 DEG C, faintly acid gas flows between hollow fiber microporous membrane element, the absorbing liquid of hollow fiber microporous membrane element surface and carbon dioxide reaction, forms a kind of weak connection compound;
H emission gases; Flue gas enters secondary heating furnace, is heated to 250 DEG C-350 DEG C, then enters air via air-introduced machine by chimney stack.
Waste-derived fuel burns the high-temperature flue gas of generation at incinerator chamber exit end desulphurization denitration, dry ice quench tower rapid cooling is entered by flue, enter cyclone dust collectors removal heavy metal, the particle that particle diameter is larger, enter depickling in half dry type extracting tower, enter activated carbon eductor adsorption particle thing, enter sack cleaner absorption flue dust, enter hollow fiber microporous membrane filtering tank removing carbon dioxide, last gas is via air-introduced machine, secondary heating furnace, chimney stack enters air, the flying dust got is collected in process, heavy metal, particle solidification process, collect the ammonium salt reprocessing of getting and become ammonia fertilizer, collect the carbon dioxide recycling got.
Steps A, desulphurization denitration.Waste-derived fuel burns the flue gas produced and stops more than 2S at incinerator chamber exit end, and temperature remains on 850 DEG C-1050 DEG C, avoids dioxin-like chemical to generate.Meanwhile, the top of incinerator chamber exit end uninterruptedly sprays ammoniacal liquor by ammonia spray device and is furnished with hoop combustion oxygen, and the acidic materials in oxygen, ammoniacal liquor and flue gas there occurs multiple reaction, and key reaction equation is as follows:
CO?+?O
2?=?CO
2
CO
2?+?2NH
3·H
2O?=?CO(NH
2)
2?+?H
2O
SO
2?+?O
2?=?SO
3
SO
2?+?2NH
3·H
2O?=?(NH
4)
2SO
3?+?H
2O
SO
2?+?NH
3·H
2O?=?NH
4HSO
3
SO
3?+?2NH
3·H
2O?=?(NH
4)
2SO
4
2NO?+?O
2?=?2NO
2
6NO?+?4NH
3·H
2O?=?5N
2?+?5H
2O
2NO
2?+?2NH
3·H
2O?=?NH
4NO
3?+?NH
4NO
2?+?H
2O
HF+?NH
3·H
2O?=?NH
4F?+?H
2O
HCL+?NH
3·H
2O?=?NH
4CL?+?H
2O
Reaction generates multiple ammonium salt, and because this step is in hot environment, water is rapidly evaporated and does not produce waste water, and the ammonium salt of generation falls into bottom conveyor, can be processed into ammonia fertilizer further.Ammonia concn, oxygen charge are according to smoke components and uninterrupted adjustment.This step can carry out desulphurization denitration at incinerator inner chamber, makes full use of the heat burning and produce, also without the need to adding catalyst, and compact conformation, cost-saving, Be very effective.
Step B, anti-dioxin.Due to the rapid gasification of cold water and dry ice, heat smoke is cooled to less than 200 DEG C in 0.5S, and before avoiding dioxin, extract generates the condition of dioxin again.Dry ice quencher, except cooling, also has dustproof function.In the process of flue gas chilling, chilled water (chw) and dry ice all gasify, and make flue gas cool-down, smaller volume, and also removing a part of flying dust is expelled to flying dust conveyer belt from quencher bottom simultaneously, treat subsequent technique solidification process.
Step C, removing heavy metals.Fully mix with the flue gas containing heavy metal after the chelating agent solution pressurization of cyclone dust collectors top spray, chelating agent and the powerful chelating of heavy metal ion, make the heavy metal ion releasing in flue gas.The pH value condition and range that chelating agent is suitable for is wide and affect little by ion concentration, can with the heavy metal ion chelating such as copper, lead, zinc, iron, cobalt, nickel, manganese, cadmium, mercury, tungsten, molybdenum, gold, silver in waste gas after form particle.Because water at high temperature gasifies, the particle that chelating is formed falls into flying dust conveyer belt, treats subsequent technique solidification process.Step C reaction temperature preferably 150 DEG C-200 DEG C, without the need to heating reactant in this temperature range, chelating agent and heavy metal ion chelating form the particle diameter of particle comparatively greatly simultaneously, and water can gasify rapidly, is beneficial to the separation that comes off of particle.
Step D, half dry type depickling.Flue gas removes after the larger particle of particle diameter through cyclone dust collectors and enters half dry type extracting tower bottom, and the atomization slaked lime slurry that tower top is gone out by nozzles spray fully contacts with the flue gas adverse current of rising, completes the absorption cleaning to flue gas acid contaminant.Half dry type depickling adopts the sour gas in slaked lime slurry and flue gas to react, and can effectively remove hydrofluoric acid, hydrogen chloride and partial CO 2.Its key reaction equation is:
2HF+?Ca(OH)
2?=?CaF
2?+?2H
2O
2HCl+?Ca(OH)
2?=?CaCl
2?+?2H
2O
CO2+?Ca(OH)
2?=?CaCO
3?+?H
2O
In half dry type extracting tower, the moisture in slaked lime slurry evaporates completely under high-temperature flue gas effect, generates without unnecessary waste water, also makes flue-gas temperature be down to less than 130 DEG C simultaneously.Reacted product is dry powder shape, and except part is expelled to subsequent technique solidification from the flying dust conveyer belt bottom half dry type extracting tower together with flying dust, all the other are extracted out by air pump from extracting tower top with flue gas.
Step e, particle-removing thing.Due to activated carbon surface loose structure, comparatively granule, ash fly and dioxin can to adsorb the heavy metal in flue gas, particle diameter further.The activated carbon granule having adsorbed pollutant is tackled by Film Filter Materials in sack cleaner, separates from flue gas, thus removes the heavy metal in flue gas further, comparatively granule, ash fly and dioxin particle diameter.Do not have the activated carbon granule of adsorption fouling thing to form filter cake on Film Filter Materials surface, can continue to adsorb the residual heavy metal of flue gas, comparatively granule, ash fly and dioxin particle diameter.
Step F, absorption flue dust.Flue gas enters from sack cleaner bottom, and temperature controls more than 60 DEG C, and in sack cleaner, polytetrafluoroethylene film filtrate filters.The acid dew point of flue gas can affect reliability and the service life of filtrate.When flue-gas temperature is lower than acid dew point, the acid solution that condensation produces is by corrosion deduster or on filtrate, form flue dust bonding and affect filter effect.After above-mentioned steps isolation of purified, flue gas acid dew point is 45 DEG C-55 DEG C, and therefore, this step temperature controls more than 60 DEG C, both without the need to additional heat flue gas, has had and can reduce the corrosion of sour gas to equipment.Further, adopt tetrafluoroethene Film Filter Materials to filter, strengthen filtrate corrosion resistance and prevent blocking.
Step G, removing carbon dioxide.Flue gas is after the deacidification of half dry type extracting tower, sack cleaner filter dirt, and the flue gas after burning flue gas is separated, and gas substantially pure only makes gas be faintly acid containing a small amount of remaining carbon dioxide.Faintly acid gas pressurized enters hollow fiber microporous membrane filtering tank, flow between hollow fiber microporous membrane element, and absorbing liquid reverse flow, carbon dioxide infiltrates layer by layer under concentration gradient effect, the absorbing liquid of hollow fiber microporous membrane element surface fully contacts with carbon dioxide, and reaction generates a kind of weak connection compound.Gas after process through secondary heating furnace again heat and detect qualified after, enter air from chimney stack.Absorbing liquid after carbon dioxide-enriched detaches hollow fiber microporous membrane element surface through liquid pump, after carrying out heat exchange, then enters desorption and regeneration in regenerator in heat exchanger with the absorbing liquid of non-absorbing carbon dioxide.
Step H, emission gases.The secondary heating furnace that gas enters clean cavity is heated to 250 DEG C-350 DEG C, and by indices detect all up to standard after, enter air by chimney stack.
Further, described waste-derived fuel incineration flue gas isolation of purified technological process adopts computer automatic control system to control, and described computer automatic control system also comprises detection system, data storage and operation display screen.
Described computer automatic control system, can to the device implementation order automatic start-stop involved by waste-derived fuel incineration flue gas isolation of purified technique, operational factor automatically detects and stores, and key parameter is carried out and automatically regulated, and makes smoke eliminator realize Automated condtrol.Computer automatic control system adopts collective and distributive type control structure, primarily of compositions such as industrial control computer system, PLC control system, field control system, data communication networks.Air-introduced machine adopts VFC, and characteristic and the load variations situation of based on fuel regulate.Pulse pocket type dust catcher deashing controls to adopt PLC control device, and control mode is timing, fixed resistance, and is provided with the detection of temperature, pressure, flow, material level, filter bag damage, realizes the supervision to system and control.
Described detection system, for the detection at the important control point of each step and the detection of final emission gases indices; Described data storage, the record for whole system service data stores; Described operation display screen, for coupled system animation, the progress situation of each step of real time inspection technological process.Further, in described steps A, ammonia supply equipment comprises ammoniacal liquor storage tank and ammoniacal liquor flow valve.Ammoniacal liquor storage tank is controlled to ammonia spray device in incinerator for ammonia by ammoniacal liquor flow valve.
Further, in described step B, the tower wall of dry ice quench tower is hollow structure, and dry ice fragment is filled in hollow layer inside, and hollow layer top connects Carbon dioxide collector.The carbon dioxide collected is recyclable.
Further, in described step D, slaked lime slurry enters agitating device and water fully stirs by the white lime be stored in white lime storehouse through blanking device, then enters rotary sprayer by white lime breast storage tank to compression pump, controls flow by rotary sprayer.
Further, in described step e, active carbon is stored in active carbon storehouse, through dispenser, air blast, sprays powdered activated carbon by active carbon nozzle to flue.Powdered activated carbon expands contact area, utilizes and absorbs.
Further, in described step F, Film Filter Materials adopts PTFE composite filtering material.The performances such as PTFE composite filtering material has high temperature resistant, corrosion-resistant, and filtering accuracy is high.
Further, the hollow fiber microporous membrane element in described step G adopts polypropylene material; Absorbing liquid adopts potassium amino acid solution; Absorbing liquid temperature is 40 DEG C-50 DEG C.
Hollow fiber microporous membrane element in described step G adopts polypropylene material; Absorbing liquid adopts potassium amino acid solution; Absorbing liquid temperature is 40 DEG C-50 DEG C.From the viewpoint of processing cost and technology stability, the material optimization polypropylene of hollow fiber microporous membrane element, absorbing liquid preferred amino acid potassium solution.Because potassium amino acid solution is the highest to the absorptivity of carbon dioxide 40 DEG C-50 DEG C time, therefore, require that hollow fiber microporous membrane filtering tank interior reaction temperature controls at 40 DEG C-50 DEG C.The heat of the heat and the loss that produce because of course of reaction is suitable, and therefore requirement enters the gas temperature of hollow fiber microporous membrane filtering tank and absorbing liquid temperature all maintains 40 DEG C-50 DEG C.
The present invention compared with prior art, has the following advantages and beneficial effect:
(1) the present invention is at burning in-furnace desulfurization, denitration, and the heat utilizing waste-derived fuel burning to produce, heats again without the need to consuming the energy, and the ammonium salt produced in desulphurization denitration process can be used for ammonia fertilizer production, and utilization rate is high.
(2) the present invention carries out rapid cooling by dry ice quench tower to the high-temperature flue gas produced in incinerator, avoids the condition that the pernicious gases such as dioxin produce, and also reduces in subsequent step and relates to the requirement of equipment to resistance to elevated temperatures.
(3) compact conformation of the present invention, avoids the generation of secondary pollution in flue gas isolation of purified process, the material optimization process after flue gas is separated.
(4) present invention process has computer controlled automatic, alleviates staff's amount of labour and work difficulty, guarantees the stability that whole system is run.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention.
Wherein: 1-incinerator; 11-ammoniacal liquor storage tank; 12-ammonia spray device; 2-dry ice quench tower; 21-Carbon dioxide collector; 3-cyclone dust collectors; 4-half dry type extracting tower; 41-white lime storehouse; 42-blanking device; 43-agitating device; 44-compression pump; 45-rotary sprayer; 5-activated carbon eductor; 51-active carbon storehouse; 52-dispenser; 53-air blast; 54-active carbon nozzle; 6-sack cleaner; 7-hollow fiber microporous membrane filtering tank; 8-secondary heating furnace; 9-air-introduced machine; 10-chimney stack.
Detailed description of the invention
Below in conjunction with embodiment, the present invention is described in further detail, but embodiments of the present invention are not limited thereto.
Embodiment 1:
The present invention is realized by following step: A desulphurization denitration; Waste-derived fuel enters incinerator 1 and burns, in incinerator 1, control temperature maintains more than 850 DEG C, the temperature of incinerator 1 chamber exit end remains on 850 DEG C-1050 DEG C, flue gas is at the incinerator 1 chamber exit end time of staying more than 2S, simultaneously, the top of incinerator 1 chamber exit end uninterruptedly sprays ammoniacal liquor by ammonia spray device and is furnished with hoop combustion oxygen, and the ammonia fertilizer of generation falls into the conveyer belt of bottom;
The anti-dioxin of B; Heat smoke enters from the top of dry ice quench tower 2, and the tower wall along embedded dry ice flows from top to bottom, flue gas and the atomization quench water co-current contact sprayed into, and due to the rapid gasification of cold water and dry ice, heat smoke is cooled to less than 200 DEG C in 0.5S;
C removing heavy metals; Flue gas through chilling enters cyclone dust collectors 3 from the bottom of dry ice quench tower 2, flue-gas temperature maintains 150 DEG C-200 DEG C, cyclone dust collectors 3 top spray chelating agent solution, the heavy metal in chelating agent pressurized liquid spray and flue gas is thoroughly mixed to form particle, and particle falls to particle conveyor;
The depickling of D half dry type; Flue gas enters from half dry type extracting tower 4 bottom, bottom half dry type extracting tower 4, rotary sprayer sprays slaked lime slurry downwards, the flue gas adverse current of slaked lime slurry solution and rising, react with the acidic materials in flue gas and generate dry powder shape material, powder falls to particle conveyor, and flue-gas temperature is down to less than 130 DEG C;
E particle-removing thing; Flue gas enters the activated carbon eductor 5 between half dry type extracting tower 4 and sack cleaner 6, sprays powdered activated carbon by active carbon nozzle 54 in flue, and the activated carbon granule of adsorbing contaminant falls to particle conveyor from activated carbon eductor 5 lower end;
F adsorbs flue dust; Flue gas enters from sack cleaner 6 bottom, and temperature controls more than 60 DEG C, and in sack cleaner 6, Film Filter Materials filters;
G removing carbon dioxide; Faintly acid gas enters hollow fiber microporous membrane filtering tank 7, temperature controls at 40 DEG C-50 DEG C, faintly acid gas flows between hollow fiber microporous membrane element, the absorbing liquid of hollow fiber microporous membrane element surface and carbon dioxide reaction, forms a kind of weak connection compound;
H emission gases; Flue gas enters secondary heating furnace 8, is heated to 250 DEG C-350 DEG C, then enters air via air-introduced machine 9 by chimney stack 10.
Embodiment 2:
The present embodiment is at the enterprising one-step optimization in the basis of above-described embodiment, further, described waste-derived fuel incineration flue gas isolation of purified technological process adopts computer automatic control system to control, and described computer automatic control system also comprises detection system, data storage and operation display screen.
Described incinerator 1 chamber exit end set temperature checkout gear and Flue valve, when incinerator 1 chamber exit end temperature being detected lower than 800 DEG C, the toxic gases such as easy generation dioxin, and the desulphurization denitration being unfavorable in catalyst-free situation, therefore send signal by control system, close Flue valve, open again until temperature reaches technological requirement.
Is provided with bypass channel in the middle of described sack cleaner 6, passage two ends arrange the valve triggered by control signal, once the flue-gas temperature entering deduster is lower than 60 DEG C, signal is sent by control system, valve transfer, flue gas passes through through bypass, extends the service life of sack cleaner 6.
The above is only preferred embodiment of the present invention, and not do any pro forma restriction to the present invention, every any simple modification, equivalent variations done above embodiment according to technical spirit of the present invention, all falls within protection scope of the present invention.
Claims (8)
1. a waste-derived fuel incineration flue gas isolation of purified technique, is characterized in that, comprise the following steps:
A desulphurization denitration; Waste-derived fuel enters incinerator (1) and burns, incinerator (1) interior control temperature maintains more than 850 DEG C, the temperature of incinerator (1) chamber exit end remains on 850 DEG C-1050 DEG C, flue gas is at incinerator (1) the chamber exit end time of staying more than 2S, simultaneously, the top of incinerator (1) chamber exit end uninterruptedly sprays ammoniacal liquor by ammonia spray device (12) and is furnished with hoop combustion oxygen, and the ammonia fertilizer of generation falls into the conveyer belt of bottom;
The anti-dioxin of B; Heat smoke enters from the top of dry ice quench tower (2), and the tower wall along embedded dry ice flows from top to bottom, flue gas and the atomization quench water co-current contact sprayed into, and due to the rapid gasification of cold water and dry ice, heat smoke is cooled to less than 200 DEG C in 0.5S;
C removing heavy metals; Flue gas through chilling enters cyclone dust collectors (3) from the bottom of dry ice quench tower (2), flue-gas temperature maintains 150 DEG C-200 DEG C, cyclone dust collectors (3) top spray chelating agent solution, heavy metal in chelating agent pressurized liquid spray and flue gas is thoroughly mixed to form particle, and particle falls to particle conveyor;
The depickling of D half dry type; Flue gas enters from half dry type extracting tower (4) bottom, half dry type extracting tower (4) bottom rotary sprayer (45) sprays slaked lime slurry downwards, the flue gas adverse current of slaked lime slurry solution and rising, react with the acidic materials in flue gas and generate dry powder shape material, powder falls to particle conveyor, and flue-gas temperature is down to less than 130 DEG C;
E particle-removing thing; Flue gas enters the activated carbon eductor (5) between half dry type extracting tower (4) and sack cleaner (6), in flue, spray powdered activated carbon by active carbon nozzle (54), the activated carbon granule of adsorbing contaminant falls to particle conveyor from activated carbon eductor (5) lower end;
F adsorbs flue dust; Flue gas enters from sack cleaner (6) bottom, and temperature controls more than 60 DEG C, and in sack cleaner (6), Film Filter Materials filters;
G removing carbon dioxide; Faintly acid gas enters hollow fiber microporous membrane filtering tank (7), temperature controls at 40 DEG C-50 DEG C, faintly acid gas flows between hollow fiber microporous membrane element, the absorbing liquid of hollow fiber microporous membrane element surface and carbon dioxide reaction, forms a kind of weak connection compound;
H emission gases; Flue gas enters secondary heating furnace, is heated to 250 DEG C-350 DEG C, then enters air via air-introduced machine (9) by chimney stack (10).
2. a kind of waste-derived fuel incineration flue gas isolation of purified technique according to claim 1, it is characterized in that: described waste-derived fuel incineration flue gas isolation of purified technological process adopts computer automatic control system to control, and described computer automatic control system also comprises detection system, data storage and operation display screen.
3. a kind of waste-derived fuel incineration flue gas isolation of purified technique according to claim 1 and 2, it is characterized in that: in described steps A, ammonia supply equipment comprises ammoniacal liquor storage tank (11) and ammoniacal liquor flow valve, and ammoniacal liquor storage tank (11) is controlled to the interior ammonia spray device (12) of incinerator (1) for ammonia by ammoniacal liquor flow valve.
4. a kind of waste-derived fuel incineration flue gas isolation of purified technique according to claim 1 and 2, it is characterized in that: in described step B, the tower wall of dry ice quench tower (2) is hollow structure, and dry ice fragment is filled in hollow layer inside, and hollow layer top connects Carbon dioxide collector (21).
5. a kind of waste-derived fuel incineration flue gas isolation of purified technique according to claim 1 and 2, it is characterized in that: in described step D, slaked lime slurry enters agitating device (43) by the white lime be stored in white lime storehouse (41) through blanking device (42) and fully stirs with water, enter rotary sprayer (45) by white lime breast storage tank, compression pump (44) again, control flow by rotary sprayer (45).
6. a kind of waste-derived fuel incineration flue gas isolation of purified technique according to claim 1 and 2, it is characterized in that: in described step e, active carbon is stored in active carbon storehouse (51), through dispenser (52), air blast (53), sprays powdered activated carbon by active carbon nozzle (54) to flue.
7. a kind of waste-derived fuel incineration flue gas isolation of purified technique according to claim 1 and 2, is characterized in that: in described step F, and Film Filter Materials adopts PTFE composite filtering material.
8. a kind of waste-derived fuel incineration flue gas isolation of purified technique according to claim 1 and 2, is characterized in that: the hollow fiber microporous membrane element in described step G adopts polypropylene material; Absorbing liquid adopts potassium amino acid solution; Absorbing liquid temperature is 40 DEG C-50 DEG C.
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| CN110864297A (en) * | 2019-11-27 | 2020-03-06 | 长兴新城环保有限公司 | Method and system for reducing dioxin in flue gas generated by waste incineration |
| CN111841298A (en) * | 2020-07-06 | 2020-10-30 | 安徽绿能技术研究院有限公司 | Enameled wire pyrolysis waste gas treatment process |
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| CN112337281A (en) * | 2020-10-26 | 2021-02-09 | 北京首钢股份有限公司 | Sintering flue gas treatment method |
| WO2022047715A1 (en) * | 2020-09-03 | 2022-03-10 | 杭州铅锂智行科技有限公司 | Method and apparatus for utilizing lead smelting tail gas treatment product |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62132523A (en) * | 1985-12-06 | 1987-06-15 | Toyobo Co Ltd | Method and device for adsorbing and removing gaseous halogenohydrocarbon |
| CN101963358A (en) * | 2010-09-30 | 2011-02-02 | 昆明理工大学 | Combined treatment method for oilfield solid waste |
| CN102225302A (en) * | 2011-03-25 | 2011-10-26 | 浙江菲达脱硫工程有限公司 | System and method for purifying tail gas of medical waste incineration |
| CN103768929A (en) * | 2014-01-28 | 2014-05-07 | 上海黎明资源再利用有限公司 | Purification treatment device for flue gas generated in garbage incineration process, and application of purification treatment device |
| CN203750409U (en) * | 2014-01-28 | 2014-08-06 | 上海黎明资源再利用有限公司 | Flue gas purifying treatment device in waste incineration process |
-
2014
- 2014-09-26 CN CN201410501011.8A patent/CN104258709B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62132523A (en) * | 1985-12-06 | 1987-06-15 | Toyobo Co Ltd | Method and device for adsorbing and removing gaseous halogenohydrocarbon |
| CN101963358A (en) * | 2010-09-30 | 2011-02-02 | 昆明理工大学 | Combined treatment method for oilfield solid waste |
| CN102225302A (en) * | 2011-03-25 | 2011-10-26 | 浙江菲达脱硫工程有限公司 | System and method for purifying tail gas of medical waste incineration |
| CN103768929A (en) * | 2014-01-28 | 2014-05-07 | 上海黎明资源再利用有限公司 | Purification treatment device for flue gas generated in garbage incineration process, and application of purification treatment device |
| CN203750409U (en) * | 2014-01-28 | 2014-08-06 | 上海黎明资源再利用有限公司 | Flue gas purifying treatment device in waste incineration process |
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| CN104728848A (en) * | 2015-04-01 | 2015-06-24 | 赵三文 | Garbage incineration device and incineration method thereof |
| CN105148705A (en) * | 2015-08-25 | 2015-12-16 | 贺州泰榕环卫设施有限公司 | Method for treating garbage incineration tail gas |
| CN105169910B (en) * | 2015-09-06 | 2018-06-15 | 中钢集团天澄环保科技股份有限公司 | Furnace flue gas dedusting and pernicious gas synergistic purification device |
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| CN105498497A (en) * | 2016-01-05 | 2016-04-20 | 中国科学院自动化研究所 | Flue gas desulfurization and denitration integrated equipment controlled through multiple variables and control method thereof |
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| CN108031230A (en) * | 2018-01-23 | 2018-05-15 | 天津城建大学 | Garbage-incineration smoke purifying device and method |
| CN109751607A (en) * | 2019-01-23 | 2019-05-14 | 民政部一零一研究所 | A kind of sacrificial offerings incinerator with flue gas purification system |
| CN110302623A (en) * | 2019-04-15 | 2019-10-08 | 杭州双良中荷环保科技有限公司 | A kind of technique of flue gas of refuse burning plasma cooperation-removal pollutant |
| CN110864297A (en) * | 2019-11-27 | 2020-03-06 | 长兴新城环保有限公司 | Method and system for reducing dioxin in flue gas generated by waste incineration |
| CN110864297B (en) * | 2019-11-27 | 2020-08-14 | 长兴新城环保有限公司 | Method and system for reducing dioxin in flue gas generated by waste incineration |
| CN111841298A (en) * | 2020-07-06 | 2020-10-30 | 安徽绿能技术研究院有限公司 | Enameled wire pyrolysis waste gas treatment process |
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| CN112337281A (en) * | 2020-10-26 | 2021-02-09 | 北京首钢股份有限公司 | Sintering flue gas treatment method |
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